Process for the production of exo-exo hexacyclic dimer of norbornadiene

ABSTRACT

Process involves the continuous production of exo-exo stereoisomer of the hexacyclic dimer of norbornadiene using a three component catalytic system of diethylaluminum chloride, ferric acetylacetonate, and bis(1,2-diphenylphosphino)ethane. Temperature range of reaction is about 100-220° F, and residence time is about 1-10 hours. Process further involves taking a product stream, along with any catalyst and other materials and treating it to deactivate the catalyst; then separating the desired exo-exo dimer by various means at a temperature below about 500° F to avoid decomposition of iron salts. Unreacted norbornadiene in the process is recycled.

CROSS REFERENCES

This application is related to the subject matter in assignee's U.S. patent application Ser. No. 640,107, filed Dec. 11, 1976.

BACKGROUND OF THE INVENTION

The invention herein described was made in the course of or under a contract thereunder with the United States Air Force Systems Command.

This invention generally relates to a process for the dimerization of norbornadiene. In particular, the invention relates to producing a hydrocarbon mixture having a high concentration of a monoolefinic hexacyclic hydrocarbon known by the systematic chemical name of exo-exo stereoisomer of hexacyclo( 7.2.1.0²,8 0.1³.7 0.1⁵.13 0.0⁴,6)tetradec-10-ene, (also designated as hexacyclo[9.2.1.0²,10 0.0³,8 0.0⁴,6 0.0⁵,9 ]tetradec-12-ene). The stereoisomer results from the catalytic dimerization of norbornadiene which is a C₇ H₈ bicyclic, diolefinic hydrocarbon. More particularly, the invention relates to a process for producing a mixture of a high concentration of the exo-exo form of the hexacyclic dimer. The latter is a C₁₄ H₁₆, six-ring monoolefinic hydrocarbon. The process can be continuous and has an advantage of recycling certain streams thereby reducing costs and increasing yields. Also, the invention relates to a process in which the product has been hydrogenated to convert the monoolefinic hexacyclics into completely saturated hexacyclics. Hydrogenation of monoolefinic hexacyclic dimer to the saturated dimer improves stability of the product towards oxidation thereby enhancing its utility as a high energy fuel. Completely saturated exo-exo hexacyclic dimer has utility as a component of high energy fuel.

An object of the present invention is to provide an economical process which can produce a composition which has a maximum concentration of hexacyclic norbornadiene dimers and a minimal concentration of pentacyclic norbornadiene dimers and other compounds. Also, the composition can be used as a component of a high energy fuel for use in either jet or rocket propulsion. Jet propulsion includes a jet engine which can be used for missile, plane and others and includes the three basic types, i.e., ramjet, turbo-jet and pulse jet. The term jet generally refers to a device requiring air whereas rocket generally refers to a device containing its own oxygen or oxidizing agent.

Norbornadiene is also known as bicyclo( 2.2.1)-heptadiene-2,5. A method of preparation is disclosed in U.S. Pat. 2,875,256 issued Feb. 24, 1959. Norbornadiene is referred to as NBD hereinafter. NBD can be represented by either one of the following structural formulas: ##STR1##

Dimerization of NBD is disclosed in U.S. Pat. No. 3,377,398, issued Apr. 9, 1968. The disclosed process results in the production of various dimer mixtures. The process therein involves the use of an iron catalyst system, e.g., ferric acetylacetonate and tirethylaluminum, and a temperature above 140° C. The product of said method is a mixture which includes both the monoolefinic hexacyclic and diolefinic pentacyclic dimers.

U.S. Pat. No. 3,282,663, issued Nov. 1, 1966, discloses the dimerization of NBD to both pentacyclic and hexacyclic dimers. In one example, tetrakis(triphenylphosphino)nickel is the catalyst, in another, iron acetylacetonate and triethylaluminum is the catalyst system. Use of cobalt acetylacetonate is suggested.

U.S. Pat. No. 3,326,992, issued June 20, 1967, discloses the partial hydrogenation of NBD dimer mixtures.

U.S. Pat. No. 3,326,993, issued June 20, 1967, discloses the dimerization of NBD, in the presence of a certain cobaltcontaining carbonyl catalyst, to heptacyclic dimers. The resulting dimer mixture contains major proportions of the completely saturated dimer.

U.S. Pat. No. 3,329,732, issued July 4, 1967, discloses an improved method for the dimerization of NBD. The catalyst comprises certain metal salts of the tetracarbonylcobaltate anion wherein the metal is zinc, cadmium, mercury or indium. Resulting dimer mixture contains predominantly hexacyclic dimers.

Catalytic reaction of NBD and butadiene is disclosed in an article in The Journal of Organic Chemistry, January, 1970, Vol. 35, title, "Catalytic Norbornadiene-Butadiene and Norbornadiene-1,1-Dimethylallene Codimerization", by A. Greco, et al., pages 271-274. One of the disclosed catalysts is a three component system of tris(acetylacetonate)Iron-AlEt₂ Cl-bis(diphenylphosphino)ethane. AlEt₂ Cl refers to diethylaluminum chloride. One of the dimers reported therein, i.e., FIG. 1e, has been identified as the exo-exo stereoisomer of hexacyclic dimer of norbornadiene.

Also, a catalytic reaction of NBD is disclosed in an article in The Journal of the American Chemical Society, Vol. 94, July 26, 1972, starting page 5446, titled, "Dimerization and Trimerization of Norbornadiene by Soluble Rhodium Catalyst", by Nancy Acton et al. This article discloses the exo-exo form of the hexacyclic dimer of NBD.

As the previous discussion indicates, many NBD dimers are possible. G. N. Schrauzer, in his review "On Transition Metal-Catalyzed Reactions of Norbornadiene and the Concept of a Complex Multicenter Processes" in Advances on Catalysis 18, 373 (1968) Acad. Press, describes the fourteen theoretically possible dimers of NBD.

Thus the process problem in the dimerization of NDB, as can be visualized from the number of possible isomers is to obtain substantial amounts of the exo-exo isomer at high yields and at reduced costs. Also, the problem is to minimize the production of pentacyclics. The latter are not desirable as high energy fuels because of their high melting points. Separation of pentacyclics from the hexacyclics is commercially not feasible. On the other hand, the exo-exo hexacyclic dimer can be easily separated from small amounts of unreacted feed and other products, particularly higher boiling polymers. Hydrogenation of the exo-exo material provides a material which can be used as a component for high energy, high density fuel.

The advantages of the present invention are many. The process can be continuous. Recycling of various streams, without build up of unwanted products, within the process reduces costs and increases yields.

SUMMARY OF THE INVENTION

The process involves the dimerization of NBD to the exo-exo form of the C₁₄ H₁₆ hexacyclic dimer. The process requires an amount of a three component catalytic system of diethylaluminum chloride, ferric acetylacetonate, and bis(1,2-diphenylphosphino)ethane sufficient to dimerize the NBD. (The three components are referred to hereinafter as DEAC, Fe(Ac)₃ and DIPHOS, respectively.) Also the process requires a temperature between the range of from about 100° F to about 220° F and sufficient residence contacting time to obtain the desired amount of exo-exo hexacyclic dimer.

A product mixture stream, along with any catalyst is removed from contacting and treated to deactivate the catalyst. The product mixture is separated from the deactivated catalyst and any other material and then the exo-exo hexacyclic dimer is obtained by separation means such as distillation from the treated product mixture. The separation steps occur at a temperature below about 500° F otherwise an iron salt decomposes and contaminates the desired dimer. Recycle of unreacted NBD, along with other materials, also occurs.

DESCRIPTION OF THE DRAWING

The accompanying drawing schematically illustrates one method carrying out the dimerization of NBD to its exo-exo hexacyclic dimer and the hydrogenation of the dimer according to the invention.

DESCRIPTION

One embodiment of the invention will be described in connection with the drawing.

The feed 1, consisting essentially of NBD, is fed to a surge device, 99 e.g. a tank. The feed is then moved to contacting means, 96 e.g. a reaction vessel. In a similar fashion DEAC 2, usually dissolved in an aromatic solvent such as toluene, is fed to a surge device 98 and then moved to the contacting means 96. Also, Fe(Ac)₃ 3 and DIPHOS 4 is fed to a surge device 97 to which is also fed NBD 5 which acts as a solvent for the Fe(Ac)₃ and DIPHOS. Other suitable solvents can be used. The resulting mixture 25 of NBD 5 and Fe(Ac)₃ 3 and DIPHOS 4 is fed to contacting means 96.

Contacting means 96 can contain agitation means, not shown, and can be equipped with sufficient heating and/or cooling means, not shown, to control the temperature of the contacting mixture. The capacity of the means 96 depends in part on the flow rate of the feed 27 and desired residence time. Residence time is defined as the volume of the contacting means 96 divided by the rate, i.e., the total volume/hour, of the materials, i.e., 27, 26, and 25, entering the contacting means 96.

Within the confines of the contacting means 96 the dimerization of the NBD to the unsaturated exo-exo hexacyclic dimer along with other polymers occurs. During the contacting the contacting mixture can be stirred and the temperature controlled within the operable range. During the contacting gases, 6 such as ethylene and/or hydrogen, can evolve. The gased can be consumed as fuel or recovered and used elsewhere. The dimerization of NBD can also be referred to as the reaction of NBD to form dimers.

Since the process can be continuous, the feed 27, DEAC 26 and catalyst mixture 25 are fed continuously to the contacting means 96 and a product mixture is continuously removed. The removed product mixture 28 is treated with a deactivator 29 e.g. an alcohol such as methanol or water. The deactivator 29 deactivates any DEAC, Fe(Ac)₃ and DIPHOS which requires deactivation. After the deactivation a sludge 8 containing aluminum hydroxide, alkyl aluminum hydroxide, insoluble polymers, and like materials is separated via separating means 94 e.g. filter device. Also during the separation some gases 7 can evolve which can be referred to as an offgas.

The treated product mixture, 9 no longer containing the sludge, is separated in separation means 93 e.g. a distillation tower. Critical to this step is that the temperature occurring during e.g. the distillation and in particular the bottoms temperature not exceed 500° F. If a higher temperature is used decomposition of an iron salt occurs and the decompostion product or products can contaminate the desired dimer. From means 93 e.g., distillation tower, a distillate 12, a overhead 10 and a bottoms 11 are obtained. The overhead 10 contains hydrocarbons and is often referred to as light ends. The distillate 12 contains the deactivator e.g. methanol or water, unreacted NBD and any solvent e.g. toluene, used with the DEAC. The bottoms 11 contains the desired dimer, by-product polymers formed during the contacting, an iron salt, DIPHOS and other like materials. The iron salt, DIPHOS and other like materials are often referred to as residue.

The distillate 12 can be further processed by feeding it to another separating means 92 e.g. a distillation device. With a distillation device an overhead 13 of methanol and/or water can be obtained and the overhead can be sent to surge means 95 along with makeup material 30. From surge means 95 can be obtained a stream of deactivator 29 which is used to treat the product mixture 28.

From separating means 92 a bottoms 14 is obtained and fed to separating means 91, e.g. a distillation device. The bottoms 14 contains unreacted NBD and solvent, if any, used with the DEAC. In separating means 91 the unreacted NBD is taken as an overhead 15 and returned to surge device 99 or to a suitable storage, not shown. In surge device 99 the recycled unreacted NBD is mixed with fresh NBD 1 and becomes a portion of feed 27. The bottoms 16 from separating means 91, is sent to another separating means 90, e.g. a distillation device, where any solvent, if used, is taken as bottoms 18 and returned to surge means 98 for reuse or to a suitable storage, not shown. In surge device 98 the recycled solvent is mixed with the DEAC and becomes a portion of feed 26. From separating means 90 an overhead 17 is obtained, the latter is referred to as slop and is any material which was carried unwanted through the previous separating means.

The bottoms 11 from the separating means 93, containing the desired dimer, by-product polymers, iron salt, DIPHOS and other like materials, is fed to separating means 89 e.g. a distillation device. An example of the latter is vacuum distillation. Critical to this step is that the temperature occurring during the distillation, and in particular the bottoms temperature, not exceed 500° F. If a higher temperature is used decomposition of an iron salt occurs and the decomposition product or products can contaminate the desired dimer. Separating means 89 effectuates the separation of the bottoms 11 into a bottoms 19 and an overhead 20. The bottoms 19 having an initial boiling point in excess of about 550° F, contains the other polymers formed and any unwanted residue. The bottoms 19 can be disposed of in a suitable manner.

The overhead 20 contains the desired dimer and has a boiling range about 450° F to about 550° F. Because the desired dimer is unsaturated the overhead 20 is fed to hydrogenation means 88, along with hydrogen 21, and hydrogenated using a typical hydrogenation catalyst such as nickel or Kieselguhr. During the hydrogenation the temperature generally does not exceed about 75° C and the hydrogen is present at about 150 psig.

The hydrogenated product 22 from the hydrogenation means 88 is sent to a separating means 87 e.g. a distillation device, to remove, which can be referred to as light ends 24, hydrogen and light hydrocarbons, if any. Bottoms 23 from the separating means 87, contains the desired saturated exo-exo hexacyclic dimer.

The catalytic dimerization of NBD via present invention can be represented by the following formula reaction: ##STR2## The dimerization requires an amount of DEAC, Fe(Ac)₃ and DIPHOS sufficient to dimerize the NBD.

The feed to present invention consists essentially of NBD. Other hydrocarbons and in particular unsaturated hydrocarbons which could react with NBD or adversely effect the catalyst and/or DEAC should be excluded. However the feed can contain minor amounts of the precursors, such as cyclopentadiene, used to make the NBD. The feed can also contain other nonreactive hydrocarbons such as toluene and benzene. Small amounts of inhibitors, such as 2,6-di-t-butyl-4-methylphenol, can be present. They inhibit formation of explosive peroxides. Very small amounts of water, e.g. about 100 ppm, can be tolerated, however, too much water can adversely effect the reaction.

The amount of DEAC, FE(Ac)₃ and DIPHOS present in the contacting zone is an effective amount so that a suitable conversion to the desired dimer occurs and the selectivity is sufficient. Any material which during the contacting could adversely effect the catalyst mixture and/or DEAC should not be presennt. For example the presence of hydroxylic compounds such as water, alcohol or oxygen from air could deactivate the catalyst mixture and/or DEAC. The concentration of the Fe(Ac)₃ during the contacting can very substantially but generally will be between the range from about 0.01 to about 0.1 gram moles per liter of contacting space; a preferred range is from about 0.02 to about 0.08. The concentration of the DIPHOS can also vary but generally is related to the amount of the Fe(Ac)₃ present, generally, its mole ratio to Fe(Ac)₃ will be between from about 1:0.5 to about 8:1; a preferred ratio of DIPHOS to Fe(Ac)₃ range is between from about 1:1 to about 6:1. The concentration of the DEAC can vary but generally its concentration during the contacting will be between the range from about 0.1 to about 1.0 gram moles per liter of contacting space; a preferred range is from about 0.2 to about 0.8.

During contacting the temperature generally will be between the range of from about 100° F to about 220° F. If a higher temperature is used the reaction could result in an uncontrolled exotherm or an undesirable amount of unwanted by-products could be made. If a lower temperature is used the reaction could be so slow as to economically unattractive. However, within the general temperature range of about 100° F to about 220° F a higher temperature can be used to lower the residence time with the contacting zone. A preferred temperature range is from about 120° F to about 200° F.

During the contacting the pressure can vary substantially; however, generally it will be in the range between from about atmospheric to about 500 psig. Pressure can help reduce the gases generated during the contacting and also faciliate the handling of any gas that does evolve. However, higher pressure can result in increased operating costs and equipment investments and thus should be minimized as long as the problems created do not offset the savings.

The residence time for the contacting depends on the volume rates of the materials fed to the contacting zone, the volume of the contacting zone, the temperature and pressure of the contacting and a result of the dimerization and other reactions. Thus the residence time can vary substantially. Generally it will be between the range from about one hour to about ten hours with a preferred range of from two hours to about eight hours.

Conversion of the NBD to the dimers depends on the aforementioned temperature range, concentrations of catalyst, the amount of agitation, residence time and other such variables. While it is desirable from an economic consideration to obtain as high a conversion as possible it is possible to optimize conversion in terms of selectivity, and minimizing unwanted byproducts, catalyst life and the like. Generally; however, the conversion of NBD to dimer will be in excess of about 50%, preferably in excess of about 75%. The variables effecting the conversion also effect the selectivity of the NBD to the exo-exo dimer. Generally the selectivity will be in excess of about 70%, preferably in excess of about 80%.

The product mixture, removed from the contacting zone and which can be cooled contains the desired exo-exo hexacyclic dimer along with the Fe(Ac)₃, DIPHOS and DEAC, and other materials. To deactivate the product mixture an alcohol such as methanol can be used. Equally effective is water including salt water. As a result of the deactivation a sludge is formed. The sludge is an undefined mixture but may include aluminum hydroxide, alkyl aluminum hydroxide, water, and other materials. And the sludge can be removed by such methods as filtration.

The treated contacting product mixture, after separation of the sludge, still contains an undefined iron salt. Thus, it is critical that the product mixture not reach a temperature which will decompose the salt.

Decomposition of the salt results in materials which contaminate the desired dimer product. Generally the maximum temperature is believed to be about 500° F; however, a preferred maximum temperature is about 475° F with 450° F more preferred.

After the separation of the unwanted materials desired exo-exo product can have a different boiling range depending on the sharpness of the preceeding separation steps. Generally, the products boiling range will be about from about 440° F to about 560° F; however, with sharper separation steps the preferred boiling range will be from about 450° F to about 550° F.

Because the desired exo-exo product is olefinic it is hydrogenated. The hydrogenation takes place in the presence of hydrogen and a hydrogenation catalyst such as nickel on kieselguhr, ruthenium on carbon, palladium on carbon, platinum oxide, palladium on alumina, ruthenium on alumina and others. The hydrogenation is generally complete so that essentially no unsaturation remains. The purpose of the hydrogenation is to replace the double bond with hydrogen thereby minimizing product degration while the product is in storage. The hydrogenation temperature and pressure can vary substantially and depend on part of the selected catalyst and decomposition temperature of the product.

The following examples serve to further illustrate applicant's invention.

EXAMPLES

The following described procedure was generally used to obtain the data reported in the accompanying Table.

Three storage containers were purged with nitrogen. DEAC, 25% by weight, dissolved in toluene, was charged to one container. The desired weights of Fe(Ac)₃ and DIPHOS were measured and charged to a preparation vessel. The charged materials were then diluted with sufficient NBD to obtain the following ratios: for Fe(Ac)₃ 44.1 mg/cc; for DIPHOS 49.8 mg/cc. The resulting mixture was warmed to facilitate the dissolving of the DIPHOS, however, some insolubles, about 0.2 wt % of the solids charged were removed by filtration. The insolubles were believed to be impurities. The filtered mixture was then charged to a container. NBD, commercially available at 97 weight % purity, was charged to another container. The impurities in the NBD were as follows: dicyclopentadiene-1 wt %; cycloheptatriene -- 1.2 wt %, toluene -- 0.1 wt %, benzene -- 0.1 wt %, other -- 0.1 wt %, inhibitor (2,6-di-t-butyl-4-methylphenol) -- 0.05 wt %. After charging the three containers were kept under nitrogen at a pressure of about 170 psig. The latter pressure was sufficient to maint n the desired flow rate to the reactor. The Fe(Ac)₃, DIPHOS and DEAC were of commercial quality.

A reaction was dried and purged with nitrogen. Product receivers, vessels which would receive product from the reactors were charged with methanol to deactivate the active materials. With runs 11 and 12 water was satisfactorly used to deactivate the active materials. NBD was fed from its container to the reaction reactor and its rate measured by a rotameter. Once the reactor was filled the NBD was fed at a rate to obtain the desired residence time and NBD/DIPHOS/--DEAC/Fe(Ac)₃ ratios. Then the DEAC solution and the FE(Ac)₃ /DIPHOS mixture were fed from their respective containers to the reaction reactor. For runs made with a residence time of 4 hours, initially the solution and the mixture were fed at a rate twice the maintenance rate for about the first 2-3 hours. Maintenance rate is that rate which maintains the desired concentration of materials in the reactor and obtains the desired residence time in the reactor. The rates were measured by a rotameter. After the first 2-3 hours the flow rates were reduced to a desired maintenance rate.

During the foregoing the temperature of the materials in the reactor were heated to the desired level by suitable heating means. Also mixing means, within the reaction reactor, maintained good mixing.

Throughout the runs flow rates and temperatures were controlled at the desired levels. Samples of reactor product were analyzed by gas chromatography (GC). When two consecutive samples gave analyses which agreed within 5% dimer conversion the unit was considered to be lined out and thus the startup period was over.

At the end of the run the product in the product receiver was removed and separated from the methanol or water and deactivated material. Samples of the product were analyzed by GC. Selectivities and conversions were calculated based on the foregoing analyses. The aforementioned results and the operating conditions are given in the accompanying table.

Comparisons of Run 1-12 indicate that % conversions were at about 60-68% with 67.5% the highest. Selectivities as to the exo-exo dimer were about 80%. Runs 11 and 12 indicate that satisfactory conversions are obtainable at low temperatures of about 120° F. Runs 2 and 3 indicate that low conversions are obtained with lower amounts of Fe(Ac)₃. For all runs wherein the selectivity to hexacyclic isomers are reported the values are at least 90% indicating minimum formation of unwanted pentacyclics.

                                      TABLE                                        __________________________________________________________________________     CONTINUOUS DIMERIZATION OPERATING CONDITIONS AND RESULTS                              Concentration                                                                  Concentration                                                                          Fe(Ac).sub.3                                                                         Concentration                                                                              Reac-   %    % Selec-                            Resi-                                                                              of      Mole  of DEAC Reac-                                                                              tor Length                                                                             Conver-                                                                             tivity                                                                              % Conver-                                                                            % Selec-                 dence                                                                              Fe(Ac).sub.3 Moles                                                                     Ratio of                                                                             Mole per                                                                               tor Pres-                                                                              of  sion of   sion                                                                                 tivity to                Time                                                                               per volume                                                                             DIPHOS/                                                                              Volume of                                                                              Temp.                                                                              sure                                                                               Run to   Exo-Exo                                                                             Trimer                                                                               Hexacyclic            Run                                                                               Hours                                                                              of Reactor                                                                             FeAc.sub.3                                                                           Reactor ° F                                                                         psig                                                                               Hours                                                                              Dimer                                                                               Dimer                                                                               Heavier                                                                              Isomers               __________________________________________________________________________     1  4   .03     1:1   0.3     180 150 4   67.5 (a)  10.1  (a)                   2  4   .015    1:1   0.3     180 150 13  33.8 79.0 trace 89.9                  3  4   .023    1:1   0.3     180 150 12  45.0 84.7 1.4   95.7                  4  4   .03     1:1   0.3     200 150 13  55.0 (a)  4.5   (a)                   5  4   .03     1:1   0.3     200 150 11  61.0 80.7 6.4   94.5                  6  4   .03     1:1   0.3     180 150 8   63.0 81.8 (a)   91.9                  7  4   .03     1:1   0.3     180 150 13  53.0 81.7 7.3   95.7                  8  4   .03     1:1   0.3     200 140 8   60.4 87.4 8.6   97.0                  9  4   --      1:1   0.3     207 130 6   65.7 81.6 9.8   94.6                  10 4   .03     1:1   0.3     200 150 10.5                                                                               64.8 82.9 8.8   97.5                  11 7.5 .03     1:1   (b)     122  26 --  50   (a)  (a)   (a)                   12 11.6                                                                               .03     1:1   (b)     121  24 --  45   (a)  (a)   (a)                   __________________________________________________________________________      (a) No data                                                                    (b) In runs 11 and 12 the mole ratio of DEAC/Fe(Ac).sub.3 was 15:1 and10:      respectively.                                                             

The invention claimed is:
 1. Process for the dimerization of norbornadiene to its exo-exo hexacyclic dimer and hydrogenation of the dimer comprising:(a) contacting a feed consisting essentially of norbornadiene with diethylaluminum chloride and a catalyst mixture of ferric acetylacetonate and bis(1,2-diphenylphosphino)ethane at a temperature between the range of from about 100° F to about 220° F and at a pressure between the range of from about atmospheric to about 500 psig and the amount of both the diethylaluminum chloride and the catalyst mixture is sufficient to dimerize the norbornadiene to the exo-exo hexacyclic dimer: (b) maintaining the contacting for a residence time sufficient to form the exo-exo hexacyclic dimer; (c) removing from the contacting a product mixture containing the formed exo-exo hexacyclic dimer and treating the mixture with methanol or water to deactivate the diethylaluminum chloride and the catalyst mixture; (d) separating from the treated contacting product mixture aluminum hydroxide sludge formed during the deactivation; (e) distilling the treated contacting product mixture from which the sludge was removed at a temperature below about 500° F to obtain both a distillate mixture and a bottom mixture wherein the distillate mixture contains any methanol or water not reacted during deactivation, unreacted norbornadiene and any solvent used with the diethaluminum chloride; and the bottom mixture contains the exo-exo hexacyclic dimer, other polymers formed during the contacting and any residue from the ferric acetylacetonate, bis(1,2 diphenylphosphino)ethane, and diethylaluminum chloride; (f) vacuum distilling the bottoms mixture at a temperature below 500° F to obtain both a distillate and bottoms and wherein the distillate has a boiling range of about 450° F to about 550° F and the bottoms has an initial boiling point of about 550° F and contains the other polymers formed and any residue; and (g) hydrogenating the about 450° F to about 550° F distillate so that essentially no unsaturation of the distillate containing the exo-exo hexacyclic dimer remains.
 2. Process according to claim 1 wherein the distillate mixture of step (e) is further distilled so that the separated methanol can be recycled to deactivate the diethylaluminum chloride and catalyst, the unreacted norbornadiene can be recycled to the contacting of step (a), and any solvent used with the diethylaluminum chloride can be recycled to dissolve the diethylaluminum chloride used in step (a).
 3. Process according to claim 1 wherein the concentration of the ferric acetylacetonate during the contacting is between the range from about 0.01 to about 0.1 grams moles per liter of contacting space and the mole ratio of the bis(1,2 diphenylphosphino)ethane to ferric acetylacetonate is between the range from about 1:0.5 to about 8:1 and the concentration of diethylaluminum chloride during the contacting is between the range from about 0.1 to about 1.0 gram moles per liter of contacting space.
 4. Process according to claim 1 wherein the conversion of norbornadiene to dimers is in excess of about 50%.
 5. Process according to claim 4 wherein the distillate mixture of step (e) is further distilled so that the separated methanol or water can be used to deactivate the diethylaluminum chloride and catalyst, the unreacted norbornadiene can be recycled to the contacting of step (a), and any solvent used with the diethylaluminum chloride can be recycled to dilute the diethylaluminum chloride used in step (a).
 6. Process according to claim 5 wherein the concentration of the ferric acetylacetonate during the contacting is between the range from about 0.01 to about 0.1 gram moles per liter of contacting space and the mole ratio of the bis(1,2 diphenylphosphino)ethane to ferric acetylacetonate is between the range from about 1:0.5 to about 8:1 and the concentration of diethylaluminum during the contacting is between the range from about 0.1 to about 1.0 gram moles per liter of contacting space. 